CN104531991B - A kind of Treating Low-grade Copper Ores Bioleaching liquid processing method - Google Patents
A kind of Treating Low-grade Copper Ores Bioleaching liquid processing method Download PDFInfo
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Abstract
The invention provides a kind of Treating Low-grade Copper Ores Bioleaching liquid processing method, phosphate method is used to realize high-efficient deferrization under the conditions of lower ph, purify leachate, and realize recycling of iron removing reagent, and pass through ultrafiltration, valuable metal in leachate (Cu) ion is simply and efficiently enriched with by Nanofiltration-membrane technique, improve follow-up extraction and electrodeposition process efficiency, additionally, the present invention also uses three-dimensional electrolysis technology to recycle raffinate, reclaim the valuable metal (Cu) in raffinate, and remove carry organic facies secretly, certain economic benefit and environmental benefit can be obtained.Whole technical process cleaning, efficiently, can make wet type copper smelting enterprise develop to the high utilization of resources and environment-friendly enterprise.
Description
Technical field
The invention belongs to field of hydrometallurgy, relate to wet type copper smelting technique, particularly to a kind of Treating Low-grade Copper Ores biology leaching
Go out liquid processing method.
Background technology
In leaching solvent extraction electrodeposition (L-SX-EW) wet type copper smelting technique, copper leachate after extraction will extraction
Remaining liquid returns and leaches, and the drawback so existed is exactly building up of the iron ion in leachate, will cause solvent extraction process
The interface emulsification phenomenon that middle appearance is serious, affects the extraction yield of copper, and by carrying secretly and entering electrodeposition system with chemical extraction after
Ferrum cathode electrode current efficiency will be caused to reduce, affect the quality of electrolytic copper.If it addition, being mingled with the raffinate of partial organic substances
By suppression Ore soaks the growth of copper antibacterial after directly spraying copper mine, affect leaching rate.In addition along with the reduction of copper ore grade,
Enter the leachate copper ion concentration requirement well below wet type copper smelting technological design of extraction process, wet type copper smelting factory production capacity
Reducing, energy consumption increases.
Summary of the invention
In view of this, it is an object of the invention to provide a kind of Treating Low-grade Copper Ores Bioleaching liquid processing method, this technique is special
It is not applicable to the pretreatment before the biochemical lixivium extraction that impurity (Fe) concentration is higher, valuable metal (Cu) ion concentration is relatively low,
And the recovery of valuable metal (Cu) ion and carry the process of organic facies secretly in raffinate.
It is an object of the invention to be achieved through the following technical solutions:
The invention provides a kind of Treating Low-grade Copper Ores Bioleaching liquid processing method, comprise the following steps:
To copper concentration be 100～2000mg/L, concentration of iron be 300～6000mg/L Treating Low-grade Copper Ores biochemical lixivium in
Add phosphate solution 2～5 times of theory demands amount (addition be), use H2SO4Solution or NaOH solution or KOH solution regulate
PH=1.4～2.7, in reaction temperature T=30～90 DEG C, rotational speed omega=80～350r/min(reactor), response time t=0.5
～carry out under the conditions of 2h except ferrum, time of repose t=0.5～1h after reaction, filter, obtain iron phosphate filtering residue and cupric filtrate；
NaOH solution or KOH solution is added, at pH=6～12, reaction temperature T=30～90 DEG C, rotating speed in phosphoric acid scum
In ω=80～350r/min(reactor), row slurrying again under the conditions of response time t=1～3h, time of repose t=0.5～1h, turn
Turning to hydrated ferric oxide. and phosphate, phosphate returns to be continuing with in initial iron removal；
Cupric filtrate is feed pressure 0.45～0.85 MPa, temperature 20～40 DEG C, and cycles of concentration is the condition of 8～10 times
Lower particle in hyperfiltration treatment, removal filtrate, obtains liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration；
Ultrafiltrated permeation liquid is feed pressure 1.25～2.05 MPa, temperature 20～40 DEG C, and cycles of concentration is the bar of 4～6 times
Concentrating through nanofiltration under part, nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；
After extraction, copper-rich organic facies enter back extraction, raffinate three-diemsnional electrode grain diameter be 3～8mm, coke 100
～300g/L or fine copper hollow bead 200～500g/L, electrolyte temperature be 20 DEG C～40 DEG C, decomposition voltage be 2.5～3.5V,
Sulfuric acid concentration is 45～100g/L, electrolysis time is 1～2h, electrolyte carries out three-dimensional electrolysis process under conditions of circulating,
Remove simultaneously and carry organic facies and deposition copper ion secretly；Lean electrolyte after three-dimensional electrolysis processes returns spray together with liquid is concentrated by ultrafiltration
Drench and leach.
Described phosphate solution is sodium radio-phosphate,P-32 solution or potassium phosphate solution.
Described three-dimensional electrolysis reactor is: the unipolarity fixed bed 3 D electrode reactor of band barrier film, in electrolysis unit
Anode use high purity graphite plate, negative electrode uses copper plate, and three-diemsnional electrode granule uses graphited coke granule or fine copper empty
Heart granule.
The present invention, relative to prior art, has the advantage that
The present invention is possible not only under the conditions of lower ph realize high-efficient deferrization, while purifying leachate, it is achieved except ferrum
Recycling of agent, and can simply and efficiently valuable metal in leachate (Cu) ion be enriched with by membrane technology,
Improve follow-up extraction and electrodeposition process efficiency, it addition, the present invention also uses three-dimensional electrolysis technology to recycle raffinate,
Reclaim the valuable metal (Cu) in raffinate, and organic facies is carried in removal secretly, can obtain certain economic benefit and environmental benefit.Whole
Individual technical process is simple to operate efficiently, and occupation area of equipment is little, and makes waste water be regenerated recycling, cleaning, efficiently, can
Wet type copper smelting enterprise is made to develop to the high utilization of resources and environment-friendly enterprise.
Accompanying drawing explanation
Fig. 1 is Treating Low-grade Copper Ores Bioleaching liquid processing method process chart of the present invention；
Fig. 2 is the three-dimensional electrolysis reactor schematic diagram that the present invention uses.
Wherein, 1 graphite electrode, 2 D.C. regulated power supplies, 3 barrier films, 4 three dimensional particles, 5 red copper negative electrodes, 6 peristaltic pumps, 7 feed liquids
Cup, 8 electrolyte.
Detailed description of the invention
Below in conjunction with the accompanying drawings and detailed description of the invention, the present invention will be further described.
As it is shown in figure 1, a kind of Treating Low-grade Copper Ores Bioleaching liquid processing method technological process of the present invention include with
Lower step:
Step 1: to copper concentration be 100～2000mg/L, concentration of iron be 300～6000mg/L Treating Low-grade Copper Ores biology leaching
Go out and liquid adds phosphate solution 2～5 times of theory demands amount (addition be), use H2SO4Solution or NaOH solution or KOH are molten
Liquid regulation pH=1.4～2.7, at reaction temperature T=30～90 DEG C, rotational speed omega=80～350r/min(in the reactor), during reaction
Between carry out except ferrum under the conditions of t=0.5～2h, time of repose t=0.5～1h after reaction, filter, obtain iron phosphate filtering residue and cupric filter
Liquid.Chemical equation such as formula (1).
Fe3++ PO4 3-+ xH2O →FePO4·xH2O↓Formula (1)
Step 2: add NaOH solution or KOH solution in phosphoric acid scum, in pH=6～12, reaction temperature T=30～90
DEG C, rotational speed omega=80～350r/min(in the reactor), under the conditions of response time t=1～3h, time of repose t=0.5～1h again
Row slurrying, is converted into hydrated ferric oxide. and phosphate, and phosphate returns to be continuing with in initial iron removal.Chemical equation is such as
Shown in formula (2).
FePO4·xH2O+OH-→ Fe(OH)3↓+PO4 3-+ xH2O formula (2)
Step 3: cupric filtrate is feed pressure 0.45～0.85 MPa, temperature 20～40 DEG C, and cycles of concentration is 8～10 times
Under conditions of through hyperfiltration treatment, remove the particle in filtrate, obtain liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration；
Step 4: ultrafiltrated permeation liquid is feed pressure 1.25～2.05 MPa, temperature 20～40 DEG C, and cycles of concentration is 4～6
Concentrating through nanofiltration under conditions of Bei, nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；
Step 5: after extraction, copper-rich organic facies enter back extraction, raffinate three-diemsnional electrode grain diameter be 3～8mm, Jiao
Charcoal 100～300g/L or fine copper hollow bead 200～500g/L, electrolyte temperature are 20 DEG C～40 DEG C, decomposition voltage be 2.5～
3.5V, sulfuric acid concentration are 45～100g/L, electrolysis time is 1～2h, electrolyte carries out three-dimensional electrolysis under conditions of circulating
Process, remove simultaneously and carry organic facies and deposition copper ion secretly.Three-dimensional electrode electrolysis technology, has specific surface area big, mass transfer velocity
Hurry up, oxidability is strong and current efficiency is high, low power consumption and other advantages, and its ultimate principle is electrocatalytic oxidation reduction reaction, by electricity
Solve, high-valence state Cu2+The granuloplastic negative electrode of three-diemsnional electrode is reduced into fine copper, the OH of lower valency-Ion is at anode graphite
O it is oxidized on plate2.And it is electrolysed generation O2With dissolving O2Negative electrode occur reduction reaction produce activity H2O2, and at metal
The effect of electrode is lower produces the hydroxyl radical free radical OH with strong oxidizing property, and the OH that reaction generates and Organic substance occur rapidly instead
It and should be made to be degraded, thus reach strengthening and remove the purpose of hardly degraded organic substance in waste water.Use DC source in acidity
Under environment, the electrode reaction being electrolysed the acid water containing copper ion is for as shown in formula (3)～formula (5).
Cathode reaction Cu2++ 2e → Cu formula (3)
Anode reaction H2O-2 e → 2H++ 1/2O2Formula (4)
Total electrode reaction Cu2++ H2O → Cu+2H++ 1/2O2Formula (5)
Step 6: the lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
Embodiment 1
The Treating Low-grade Copper Ores biochemical lixivium that the present invention processes, original liquid component Cu2+=0.14g/L, Fe3+=0.5g/L, pH=
2.2, in Treating Low-grade Copper Ores biochemical lixivium, add sodium radio-phosphate,P-32 solution, sulphuric acid regulation pH=1.5, reaction temperature T=30 DEG C, rotating speed
ω=300r/min, after response time t=0.5h, time of repose t=0.5h, filters, obtains iron phosphate filtering residue and cupric filtrate, remove
Ferrum rate 99%, copper loss rate 2%.Phosphoric acid scum adds sodium hydroxide solution, in pH=10 reaction temperature T=80 DEG C, rotational speed omega=
Under the conditions of 300r/min, response time t=2h, time of repose t=0.5h, filter, be allowed to be converted into ferric hydroxide precipitate and phosphoric acid
Sodium solution, sodium radio-phosphate,P-32 solution returns to initial iron removal and is continuing with, the phosphate radical response rate 95%.
Cupric filtrate is feed pressure 0.65 MPa, temperature 30 DEG C, and cycles of concentration is 10 times and carries out hyperfiltration treatment, removes filter
Particle in liquid, obtains liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration.After hyperfiltration treatment, Cu in ultrafiltrated permeation liquid2+=0.13g/L。
Ultrafiltrated permeation liquid is feed pressure 1.50MPa, temperature 30 DEG C, and cycles of concentration carries out nanofiltration concentration under the conditions of being 5 times,
Nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；Cu in nanofiltration concentrated solution2+=0.63g/L。
After extraction, copper-rich organic facies enters back extraction, and raffinate composition is Cu2+=0.15g/L, Organic substance and oil content exist
400～500ppm, it is added thereto to sulphuric acid and makes its sulfuric acid concentration be 85g/L, the anode in electrolysis unit uses high purity graphite plate,
Negative electrode uses copper plate, and three-diemsnional electrode granule uses graphited coke granule, and particle diameter is 5mm, and electrolyte circulates, at electricity
Solve voltage U=3.5V, electrolyte temperature 30 DEG C, coke 150g/L, under the conditions of electrolysis time t=1h after three-dimensional electrolysis processes, have
Machine thing and oil content 40～50ppm, copper recovery 99%.
Lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
Embodiment 2
The Treating Low-grade Copper Ores biochemical lixivium that the present invention processes, original liquid component Cu2+=0.28g/L, Fe3+=0.6g/L, pH=
2.5, in Treating Low-grade Copper Ores biochemical lixivium, add sodium radio-phosphate,P-32 solution, sulphuric acid regulation pH=1.8, reaction temperature T=30 DEG C, rotating speed
ω=300r/min, after response time t=0.5h, time of repose t=0.5h, filters, obtains iron phosphate filtering residue and cupric filtrate, remove
Ferrum rate 99%, copper loss rate 2%.Phosphoric acid scum adds sodium hydroxide solution, in pH=10 reaction temperature T=80 DEG C, rotational speed omega=
Under the conditions of 300r/min, response time t=2h, time of repose t=0.5h, filter, be allowed to be converted into ferric hydroxide precipitate and phosphoric acid
Sodium solution, sodium radio-phosphate,P-32 solution returns to initial iron removal and is continuing with, the phosphate radical response rate 95%.
Cupric filtrate is feed pressure 0.65 MPa, temperature 30 DEG C, and cycles of concentration is 10 times and carries out hyperfiltration treatment, removes filter
Particle in liquid, obtains liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration.After hyperfiltration treatment, Cu in ultrafiltrated permeation liquid2+=0.27g/L。
Ultrafiltrated permeation liquid is feed pressure 1.50MPa, temperature 30 DEG C, and cycles of concentration carries out nanofiltration concentration under the conditions of being 4 times,
Nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；Cu in nanofiltration concentrated solution2+=1.06g/L。
After extraction, copper-rich organic facies enters back extraction, and raffinate composition is Cu2+=0.19g/L, Organic substance and oil content exist
400～500ppm, it is added thereto to sulphuric acid and makes its sulfuric acid concentration be 85g/L, the anode in electrolysis unit uses high purity graphite plate,
Negative electrode uses copper plate, and three-diemsnional electrode granule uses fine copper hollow bead, and particle diameter is 6mm, and electrolyte circulates, at electrolysis electricity
Pressure U=3.5V, electrolyte temperature 30 DEG C, fine copper hollow bead 300g/L, process through three-dimensional electrolysis under the conditions of electrolysis time t=1h
After, Organic substance and oil content 40～50ppm, copper recovery 99%.
Lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
Embodiment 3
The Treating Low-grade Copper Ores biochemical lixivium that the present invention processes, original liquid component Cu2+=0.19g/L, Fe3+=0.6g/L, pH=
2.3, in Treating Low-grade Copper Ores biochemical lixivium, add potassium phosphate solution, sulphuric acid regulation pH=1.5, reaction temperature T=30 DEG C, rotating speed
ω=300r/min, after response time t=0.5h, time of repose t=0.5h, filters, obtains iron phosphate filtering residue and cupric filtrate, remove
Ferrum rate 99%, copper loss rate 2%.Phosphoric acid scum adds potassium hydroxide solution, in pH=10 reaction temperature T=80 DEG C, rotational speed omega=
Under the conditions of 300r/min, response time t=2h, time of repose t=0.5h, filter, be allowed to be converted into ferric hydroxide precipitate and phosphoric acid
Potassium solution, potassium phosphate solution returns to initial iron removal and is continuing with, the phosphate radical response rate 95%.
Cupric filtrate is feed pressure 0.65 MPa, temperature 30 DEG C, and cycles of concentration is 10 times and carries out hyperfiltration treatment, removes filter
Particle in liquid, obtains liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration.After hyperfiltration treatment, Cu in ultrafiltrated permeation liquid2+=0.18g/L。
Ultrafiltrated permeation liquid is feed pressure 1.60MPa, temperature 30 DEG C, and cycles of concentration carries out nanofiltration concentration under the conditions of being 6 times,
Nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；Cu in nanofiltration concentrated solution2+=1.05g/L。
After extraction, copper-rich organic facies enters back extraction, and raffinate composition is Cu2+=0.16g/L, Organic substance and oil content exist
400～500ppm, it is added thereto to sulphuric acid and makes its sulfuric acid concentration be 100g/L, the anode in electrolysis unit uses high purity graphite
Plate, negative electrode uses copper plate, and three-diemsnional electrode granule uses graphited coke granule, and particle diameter is 5mm, and electrolyte circulates,
At decomposition voltage U=3.5V, electrolyte temperature 30 DEG C, coke 150g/L, process through three-dimensional electrolysis under the conditions of electrolysis time t=1h
After, Organic substance and oil content 40～50ppm, copper recovery 99%.
Lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
Embodiment 4
The Treating Low-grade Copper Ores biochemical lixivium that the present invention processes, original liquid component Cu2+=0.31g/L, Fe3+=0.7g/L, pH=
2.2, in Treating Low-grade Copper Ores biochemical lixivium, add potassium phosphate solution, sulphuric acid regulation pH=1.5, reaction temperature T=30 DEG C, rotating speed
ω=300r/min, after response time t=0.5h, time of repose t=0.5h, filters, obtains iron phosphate filtering residue and cupric filtrate, remove
Ferrum rate 99%, copper loss rate 2%.Phosphoric acid scum adds sodium hydroxide solution, in pH=10 reaction temperature T=80 DEG C, rotational speed omega=
Under the conditions of 300r/min, response time t=2h, time of repose t=0.5h, filter, be allowed to be converted into ferric hydroxide precipitate and phosphoric acid
Potassium solution, potassium phosphate solution returns to initial iron removal and is continuing with, the phosphate radical response rate 95%.
Cupric filtrate is feed pressure 0.65 MPa, temperature 30 DEG C, and cycles of concentration is 10 times and carries out hyperfiltration treatment, removes filter
Particle in liquid, obtains liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration.After hyperfiltration treatment, Cu in ultrafiltrated permeation liquid2+=0.30g/L。
Ultrafiltrated permeation liquid is feed pressure 1.60MPa, temperature 30 DEG C, and cycles of concentration carries out nanofiltration concentration under the conditions of being 4 times,
Nanofiltration concentrated solution enters extraction process, and nanofiltration penetrating fluid returns and produces reuse；Cu in nanofiltration concentrated solution2+=1.16g/L。
After extraction, copper-rich organic facies enters back extraction, and raffinate composition is Cu2+=0.18g/L, Organic substance and oil content exist
400～500ppm, it is added thereto to sulphuric acid and makes its sulfuric acid concentration be 100g/L, the anode in electrolysis unit uses high purity graphite
Plate, negative electrode uses copper plate, and three-diemsnional electrode granule uses fine copper hollow bead, and particle diameter is 6mm, and electrolyte circulates, at electricity
Solving voltage U=3.5V, electrolyte temperature 30 DEG C, fine copper hollow bead 300g/L, under the conditions of electrolysis time t=1h at three-dimensional electrolysis
After reason, Organic substance and oil content 40～50ppm, copper recovery 99%.
Lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
It should be noted last that: above example is merely to illustrate and unrestricted technical scheme, simply according to
This method is described in detail by examples detailed above, and those skilled in the art is to be understood that.Still the present invention can be carried out
Amendment or equivalent, any amendment without departing from the spirit and scope of the present invention and local are replaced, and it all should be contained
Among scope of the presently claimed invention.
Claims (7)
1. a Treating Low-grade Copper Ores Bioleaching liquid processing method, it is characterised in that comprise the following steps:
Step 1: to copper concentration be 100～2000mg/L, concentration of iron be 300～6000mg/L Treating Low-grade Copper Ores biochemical lixivium
The phosphate solution of 2～5 times of middle addition theory demands amount, uses H2SO4Solution or NaOH solution or KOH solution regulate pH=1.4
～2.7, in reaction temperature T=30～90 DEG C, rotational speed omega=80 of reactor～350r/min, response time t=0.5～2h condition
Under carry out except ferrum, time of repose t=0.5～1h after reaction, filter, obtain iron phosphate filtering residue and cupric filtrate；
Step 2: add NaOH solution or KOH solution in iron phosphate filtering residue, pH=6～12, reaction temperature T=30～90 DEG C,
Row slurrying again under the conditions of rotational speed omega=80 of reactor～350r/min, response time t=1～3h, time of repose t=0.5～1h,
Being converted into hydrated ferric oxide. and phosphate, phosphate returns to be continuing with in initial iron removal；
Step 3: cupric filtrate is feed pressure 0.45～0.85 MPa, temperature 20～40 DEG C, and cycles of concentration is the bar of 8～10 times
Through hyperfiltration treatment under part, remove the particle in filtrate, obtain liquid and ultrafiltrated permeation liquid are concentrated by ultrafiltration；
Step 4: ultrafiltrated permeation liquid is feed pressure 1.25～2.05 MPa, temperature 20～40 DEG C, and cycles of concentration is 4～6 times
Under the conditions of through nanofiltration concentrate, nanofiltration concentrated solution enter extraction process, nanofiltration penetrating fluid return produce reuse；
Step 5: after extraction, copper-rich organic facies enters back extraction, and raffinate enters 3 D electrode reactor and is electrolysed, three-dimensional electricity
Pole reactor uses the unipolarity fixed bed 3 D electrode reactor of band barrier film, and the anode in 3 D electrode reactor uses high-purity
Graphite cake, negative electrode uses copper plate, and three-diemsnional electrode granule uses graphited coke granule or fine copper hollow bead；Three-dimensional electrolysis
Condition: grain diameter is 3～8mm, coke 100～300g/L or fine copper hollow bead 200～500g/L, electrolyte temperature are 20
DEG C～40 DEG C, decomposition voltage be 2.5～3.5V, sulfuric acid concentration be 45～100g/L, electrolysis time be 1～2h, electrolyte circulation
Carry out three-dimensional electrolysis process under conditions of flowing, remove simultaneously and carry organic facies and deposition copper ion secretly；
Step 6: the lean electrolyte after three-dimensional electrolysis processes returns shower-bubble type together with liquid is concentrated by ultrafiltration.
Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that: described in step 1
Phosphate solution is sodium radio-phosphate,P-32 solution or potassium phosphate solution, and addition is 3～5 times of theory demands amount.
Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that: Treating Low-grade Copper Ores is raw
Thing leachate regulation pH=1.6～2.7, at reaction temperature T=50～90 DEG C, rotational speed omega=150～350r/min, response time t=
Carry out under the conditions of 0.7～2h except ferrum, time of repose t=0.9～1h after reaction.
Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that: in phosphoric acid scum
Add NaOH solution or KOH solution, at pH=8～12, reaction temperature T=40～90 DEG C, rotational speed omega=100 of reactor～350r/
Row slurrying again under the conditions of min, response time t=1.5～3h, time of repose t=0.8～1h.
Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that: cupric filtrate is being entered
Material pressure 0.50～0.85 MPa, temperature 30～40 DEG C, cycles of concentration be 8～10 times under conditions of through hyperfiltration treatment.
A kind of Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that ultrafiltration is permeated
Liquid is feed pressure 1.75～2.05 MPa, temperature 30～40 DEG C, and cycles of concentration concentrates through nanofiltration under conditions of being 4～6 times.
Treating Low-grade Copper Ores Bioleaching liquid processing method the most according to claim 1, it is characterised in that described in step (5)
Three-dimensional electrolysis condition is: grain diameter is 5～8mm, coke 150～300g/L or fine copper hollow bead 250～500g/L, electrolysis
Liquid temp is 25 DEG C～40 DEG C, decomposition voltage is 2.5～3.5V, sulfuric acid concentration is 45～100g/L, electrolysis time is 1～2h,
Electrolyte carries out three-dimensional electrolysis process under conditions of circulating.
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| AR109192A1 (en) * | 2016-08-08 | 2018-11-07 | Enirgi Know How Pte Ltd | A PROCESS FOR THE CONVERSION OF LITHIUM PHOSPHATE IN A LOW SOLUTION OF APPROPRIATE LITHIUM PHOSPHATE AS A RAW MATERIAL FOR THE PRODUCTION OF VENDABLE LITHIUM PRODUCTS AND FOR THE RECOVERY OF PHOSPHORY FOR RE-USE IN THE PRODUCTION OF LITHIUM PHOSPHATE |
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| CN112575202A (en) * | 2020-11-17 | 2021-03-30 | 金川集团股份有限公司 | Method for purifying nickel-cobalt solution and recovering iron |
| CN115927861A (en) * | 2023-02-01 | 2023-04-07 | 福建百灵天地环保科技有限公司 | Process for extracting metal copper from copper-containing acidic mine wastewater |
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